Desalination system and desalination method

ABSTRACT

This desalinization system, which obtains industrial-use water and drinking water from seawater and wastewater, is provided with: a purification device that purifies wastewater by removing activated sludge therefrom; a first RO membrane that removes salt from the output of the purification device by transferring said salt to first concentrated water, thereby producing industrial-use water; a UF membrane that seawater passes through and that removes particulates from said seawater; a second RO membrane that removes salt from the treated output of the UF membrane by transferring said salt to second concentrated water, producing drinking water; an agitation device to which the second concentrated water from the second RO membrane and the first concentrated water from the first RO membrane are sent to be agitated; and a third RO membrane removing salt from the liquid mixture agitated by the agitation device by transferring said salt to third concentrated water, producing industrial-use water.

TECHNICAL FIELD

This application is a Divisional of application Ser. No. 14/232,955filed Jan. 15, 2014, which is a National Stage Application ofPCT/JP2012/070792 filed Aug. 16, 2012. The entire disclosures of theprior applications are hereby incorporated by reference herein in theirentirety.

The present invention relates to a sea-water desalination system fordesalinating sea-water and sewage water and a sea-water desalinationmethod.

BACKGROUND ART

Recently, due to the global growth of population and the broadindustrial developments including emerging countries, thefresh-water-generation demands of the drinking water and the industrialwater in the desert areas or the like have become definite.

Formerly, there has been a desalination system S100 shown in FIG. 5, asa system for desalinating the sea-water and the sewage water.

The production of the product water s101 (the industrial water)utilizing the sewage water in the desalination system S100 is executedas following. Incidentally, the salinity concentration of the sewagewater is approximately 0.1%.

The sewage water is water-supplied to the MBR (Membrane Bioreactor) 101by the pump p101, and the activated sludge or the like of the solidcontents in the sewage water is removed by the MBR 101, then the MBRpermeable water which has permeated the MBR 101 is water-supplied to thelow-pressure RO membrane (Reverse Osmosis Membrane) 102 by the pumpp102.

Incidentally, the MBR permeable water which has permeated the MBR 101has the salinity concentration of approximately 0.1% which is low,therefore, as the RO membrane, the low-pressure RO membrane 102 which isan RO membrane (reverse osmosis membrane) of the low-pressure ofapproximately 1 to 2 MPa (mega-pascal) is utilized.

By permeating the low-pressure RO membrane 102, almost a half of theconcentrated-water s104 including the impurities of the salinity or thelike is removed, and the MBR permeable water water-supplied by the pumpp102 is desalinated, then the industrial water of the remaining half ofproduct water s101 is produced.

To the contrary, the concentrated-water s104 which includes theimpurities of the salinity or the like removed by the low-pressure ROmembrane 102 and is approximately ½ in volume of the sewage waterconcentrated to the salinity concentration of approximately 0.2%, iswater-supplied from the low-pressure RO membrane 102 to thestirring-vessel 104.

The production of the industrial water which is the product water s102from the sea-water in the desalination system S100 is executed asfollowing. Incidentally, the salinity concentration of the sea-water is3 to 4% approximately.

The sea-water is water-supplied to the UF membrane 103 by the pump p103,and water-supplied to the stirring-vessel 104, removing particles by theUF membrane 103. In the stirring-vessel 104, the UF membrane permeationsea-water which has permeated this UF membrane 103 and theconcentrated-water s104 which is approximately ½ in volume of the sewagewater concentrated from the sewage water by the aforementionedlow-pressure RO membrane 102 are stirred and water-supplied to theintermediate-pressure RO membrane 105 by the pump p104, thereafter.

The UF membrane permeation sea-water which has permeated the UF membrane103 has the salinity concentration of 3 to 4%, however, it is diluted bythe concentrated-water s104 of the salinity concentration of 0.2%,accordingly, the intermediate-pressure RO membrane 105 of the ROmembrane (reverse osmosis membrane) of approximately 3 to 5 MPa of theintermediate-pressure is utilized.

Of the mixture water s103 which has been water-supplied from thestirring-vessel 104 to the intermediate-pressure RO membrane 105 by thepump p104, by permeating the intermediate-pressure RO membrane 105,approximately ½ is removed as the brine water s105 including theimpurities of the salinity or the like, and the remaining approximately½ is produced as the desalinated product water s102 (the industrialwater). In other words, the industrial water of the product water s102is produced as ½ of the sea-water plus approximately ¼ of the sewagewater in volume.

To the contrary, the brine water s105 which has been concentrated in theapproximately twice the salinity concentration of the mixture water s103including the impurities of the salinity or the like removed by theintermediate-pressure RO membrane 105, is removed from theintermediate-pressure RO membrane 105. In other words, the brine waters105 is drained as ½ of the sea-water plus approximately ¼ of the sewagewater in volume.

Incidentally, the pressure energy of the brine water s105 is recoveredas the rotational energy by the energy recovery device 106, and isutilized as the power source (energy source) of the pressure-transfer tothe intermediate-pressure RO membrane 10 of a part of the mixture waters103 which has by-passed the pump p104.

As another conventional desalination system, there is a desalinationsystem S200 shown in FIG. 6.

The desalination system S200 doesn't supply the concentrated-water s104of the sewage water in the desalination system S100 of FIG. 5 to thestirring-vessel 204, and constitutes the desalination of the sewagewater and the desalination of the sea-water independently.

In the desalination system S200, the sea-water with the high thesalinity concentration is not diluted by the supply from the sewagewater (the concentrated-water s104 of the sewage water of FIG. 5) by thestirring-vessel 204, therefore, the high-pressure RO membrane 205 whichhas the salinity concentration as high as approximately 3 to 4% and thehigh-pressure of approximately 6 to 8 MPa is utilized.

The other configuration is similar to the desalination system S100 ofFIG. 5, accordingly, the components of the desalination system S100 areshown with references in the two-hundred range and the in-depthdescriptions are omitted.

In the desalination system S200, the sewage water permeates thelow-pressure RO membrane 202 and is desalinated, and the industrialwater which is the product water s201 of approximately a half of thesewage water can be acquired. To the contrary, the sea-water permeatesthe high-pressure RO membrane 205 and is desalinated, and the drinkingwater which is the product water s202 of a ½ amount of the sea-water canbe acquired.

The conventional desalination system S100 (See FIG. 5) has followingadvantages, compared to the desalination system S200 (See FIG. 6).

Firstly, in the desalination system S100 of FIGS, the drainage (theconcentrated-water s104) removed in the process forfresh-water-generating the product water s101 from the sewage water isutilized in the process for fresh-water-generating the product waters102 from the sea-water, therefore, there are advantages to be capableof increasing the production amount of the product water from thesea-water.

More specifically, in the case not to utilize the drainage (theconcentrated-water s104) from the sewage water, regarding the productwater from the sea-water, it is possible to water-intake more industrialwater of the product water s102 as much as the water-increased volume ofapproximately ½ of the sewage water, in place of the approximately ½ ofthe sea-water in volume.

Secondly, regarding the sea-water (the salinity concentration 3 to 4%approximately), the concentrated-water s104 (the salinity concentration0.2% approximately) in the low-pressure RO membrane 102 of the sewagewater is added, therefore, the sea-water is diluted and the salinityconcentration is decreased. Therefore, in the case not to utilize thedrainage (the concentrated-water s104) from the sewage water, thehigh-pressure RO membrane was required because the sea-water has thehigh the salinity concentration, however, due to the dilution by theconcentrated-water s104, the intermediate-pressure RO membrane 105 issufficient, and the power of the pump p104 can be decreased, compared tothe case of the high-pressure RO membrane.

Incidentally, in comparison with the permeation pressure of theintermediate-pressure RO membrane of approximately 3 to 5 MPa, thepermeation pressure of the high-pressure RO membrane is approximately 6to 8 MPa, and in order to permeate the high-pressure RO membrane, thelarger power (energy) than the intermediate-pressure RO membrane isrequired.

Incidentally, there is Patent Literature 1 as a prior art reference inrespect of the present invention.

PRIOR ART REFERENCE

Patent Literature

[Patent Literature 1] JP 4481345 A

SUMMARY OF THE INVENTION Problems to be Solved by the Invention

Incidentally, the conventional desalination system S100 shown in FIG. 5has following problems.

Firstly, there is generally a large demand of the drinking water,however, it is impossible to produce the drinking water from thesea-water, in order to mix a part of the sewage water (theconcentrated-water s104) in the process for desalinating the sea-water.Secondly, though the supply amount of the sea-water is normally largecompared to the supply amount of the sewage water in many cases, in thecase that the supply amount of the sea-water is large, the effect to addthe sewage water in the process for desalinating the sea-water,decreases.

More specifically, in the case that the supply amount of the sea-wateris large, even if a part of the sewage water is added to the process fordesalinating the sea-water, the relative amount to the sea-water issmall, therefore, the salinity concentration doesn't decrease so much,and the reduction effect of the permeation pressure to the RO membrane(corresponding to the intermediate-pressure RO membrane 105 of FIG. 5)for desalinating, decreases. As a result, the power (energy) reductioneffect for acquiring the permeation pressure of the RO membrane,decreases. In addition, the water-increase effect of the product waters102 also decreases.

Thirdly, the energy recovery device 106 shows the higher efficiency inthe high-pressure cases, however, since the intermediate-pressure ROmembrane 105 is utilized, the energy recovery device 106 cannot beoperated in the high efficiency zone. Therefore, it is difficult toacquire the high energy recovery ratio.

Fourthly, it is hard to mention that the maintainability is Favorable,since the different reverse osmosis membranes of the low-pressure ROmembrane 102 and the intermediate-pressure RO membrane 105 are utilized.

An object of the present invention is, in respect of the aforementionedactual condition, to provide a sea-water desalination system and asea-water desalination method which are possible to produce the drinkingwater from the sea-water and also to water-increase the industrial waterwith inexpensive fresh-water-generation costs.

Means for Solving the Problem

In order to achieve the aforementioned purpose, a sea-water desalinationsystem according to system A is a sea-water desalination system foracquiring the industrial water and the drinking water from the sea-waterand the sewage water, comprising: a purification apparatus for removingactivated sludge by permeating the sewage water and purifying; a firstRO membrane for permeating the permeable water which permeated thepurification apparatus and including and removing salinity thereof infirst concentrated-water and also generating the industrial water; a UFmembrane for removing particles in the sea-water by permeating thesea-water; a second RO membrane for permeating treated water whichpermeated the UF membrane and including and removing salinity of thetreated water in second concentrated-water and also generating drinkingwater; a stirring apparatus for stirring the second concentrated-waterremoved by the second RO membrane and the first concentrated-waterremoved by the first RO membrane being sent thereto; and a third ROmembrane for permeating mixture fluid stirred by the stirring apparatus,and including and removing salinity thereof in third concentrated-waterand also generating the industrial water.

A sea-water desalination method according to method A is a method torealize a sea-water desalination system according to system A.

Method A is sea-water desalination method for acquiring industrial waterand drinking water from sea-water and sewage water, producing industrialwater by making the sewage water permeate purification apparatus andfirst RO membrane; producing drinking water by making the sea-waterpermeate UF membrane and second RO membrane; and producing industrialwater by making mixture fluid which mixed first concentrated-waterremoved by the first RO membrane and the second concentrated-waterremoved by the second RO membrane permeate third RO membrane.

A sea-water desalination system according to system B is a sea-waterdesalination system for acquiring the industrial water and the drinkingwater from the sea-water and the sewage water, comprising: apurification apparatus for removing activated sludge by permeating thesewage water and purifying; a UF membrane for removing particles in thesea-water by permeating the sea-water; a first RO membrane forpermeating treated water which permeated the UF membrane and includingand removing salinity of the treated water in first concentrated-waterand also generating the drinking water; a stirring apparatus forstirring the first concentrated-water removed by the first RO membraneand the treated water which permeated the purification apparatus beingsent thereto; and a second RO membrane for permeating the mixture fluidstirred by the stirring apparatus, and including and removing salinitythereof in second concentrated-water and also generating the industrialwater.

A sea-water desalination method according to method B is a method torealize a sea-water desalination system according to system B.

Method B is a sea-water desalination method for acquiring industrialwater and drinking water from sea-water and sewage water, removingactivated sludge and purifying by making the sewage water permeatepurification apparatus; producing drinking water by making the sea-waterpermeate UF membrane and first RO membrane; and producing industrialwater by making mixture fluid which mixed first concentrated-waterremoved by the first RO membrane and the treated water which permeatedthe purification apparatus permeate second RO membrane.

Effect of the Invention

The sea-water desalination system and the sea-water desalination methodof the present invention can realize the sea-water desalination systemand the sea-water desalination method Which are capable of producing thedrinking water from the sea-water and also to water-increase theindustrial water with inexpensive fresh-water-generation costs.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a conceptual configuration diagram of the desalination systemof the embodiment 1 with reference to the present invention;

FIG. 2 is a conceptual configuration diagram showing the desalinationsystem of the embodiment 2;

FIG. 3 is a conceptual configuration diagram showing the desalinationsystem of the variation 1;

FIG. 4 is a conceptual configuration diagram showing the desalinationsystem of the variation 2;

FIG. 5 is a conceptual configuration diagram showing the conventionaldesalination system; and

FIG. 6 is a conceptual configuration diagram showing the otherconventional desalination system.

MODES FOR CARRYING OUT THE INVENTION

Hereinafter, the embodiments of the present invention are described withreference to the attached drawings.

Embodiment 1

FIG. 1 is a conceptual configuration diagram of the desalination systemof the embodiment 1 with reference to the present invention.

The desalination system S of the embodiment 1 comprises an MBR (MembraneBioreactor) 1 for removing the activated sludge or the like from thesewage water and purifying, and a low-pressure RO membrane (ReverseOsmosis Membrane) 2 for removing the impurities of the salinity, ions orthe like included in the sewage water and desalinating, in order toproduce the industrial water s1 from the sewage water.

The MBR 1 performs the solid-liquid separation, removes the activatedsludge or the like (solid contents, bacteria or the like) from thesewage water, and purifies.

The RO membrane (reverse osmosis membrane) is a semipermeable membraneto pass water, however, hardly to pass low molecular substances of thesalinity or the like and ions. The low-pressure RO membrane 2 is alow-pressure RO membrane for removing the salinity or the like by thepermeation pressure approximately 1 to 2 MPa (mega-pascal) which isrelatively low, since the salinity concentration of the sewage water is0.1% approximately, which is low.

Furthermore, the desalination system S comprises a UF membrane(Ultrafiltration Membrane) 3 for removing the particles included in thesea-water, and a high-pressure RO membrane 4 for removing the salinityincluded in the sea-water and the impurities of the ions or the like anddesalinating, in order to produce the drinking water s2 from thesea-water.

The UF membrane (ultrafiltration membrane) 3 performs the screening ofthe molecule levels depending on the pore size of the membrane and themolecule size of the to-be-excluded substances in the sea-water, andremoves the substances which are to-be-excluded.

The high-pressure RO membrane 4 is a high-pressure RO membrane forremoving the salinity or the like by the relatively high permeationpressure of approximately 6 to 8 MPa (mega-pascal), since the salinityconcentration of the sea-water is 3 to 4% approximately.

Furthermore, in order to produce the industrial water s3 from thesea-water, in addition to the aforementioned UF membrane 3 and thehigh-pressure RO membrane 4, the desalination system S comprises astirring-vessel 5 for stirring the sea-water concentrated-water s7including the salinity and the impurities of ions or the like removedfrom the high-pressure RO membrane 4 and the sewage waterconcentrated-water s6 including the salinity and the impurities of ionsor the like removed from the low-pressure RO membrane 2, and ahigh-pressure RO membrane 6 for removing the salinity and the impuritiesof ions or the like included in the mixture fluid from thestirring-vessel 5 and desalinating.

The high-pressure RO membrane 6 desalinates the mixture fluid of thesea-water concentrated-water s7 of the salinity concentration(approximately 6 to 8% salinity concentration) which is almost twice ofthe sea-water and the sewage water concentrated-water s6 of the salinityconcentration (approximately 0.2% salinity concentration) which isalmost twice of the sewage water, and is a high-pressure RO membrane forremoving the salinity or the like by the relatively high permeationpressure, approximately 6 to 8 MPa (mega-pascal) thereby. Incidentally,the sea-water concentrated-water s7 of the salinity concentration ofapproximately 6 to 8% which is almost twice of the sea-water, is dilutedby adding the sewage water concentrated-water s6 (approximately 0.2%salinity concentration) and the salinity concentration is decreased.

Subsequently, a process for fresh-water-generating the industrial waters1 from the sewage water in the desalination system S is described.

The sewage water is water-supplied to the MBR 1 by the pump p1 andpermeates the MBR 1, and the activated sludge flocks, bacteria and thelike are removed from the sewage water. The MBR permeable water s5 a ofthe sewage water which has permeated the MBR 1 is water-supplied to thelow-pressure RO membrane 2 by the pump p2, and the sewage waterconcentrated-water s6 including the impurities of the salinity, ions orthe like is removed and desalinated by permeating the low-pressure ROmembrane 2, then the industrial water s1 is produced.

In the industrial water s1, while approximately ½ of the sewage watercan be acquired, the remainder of the sewage water, that is to say,approximately ½ of the sewage water is removed as the sewage waterconcentrated-water s6 including the impurities of the salinity, ions orthe like.

The sewage water concentrated-water s6 which includes the impurities ofthe salinity, ions or the like removed by the low-pressure RO membrane 2and is concentrated to the salinity concentration of 0.2% approximately,is water-Supplied from the low-pressure RO membrane 2 to thestirring-vessel 5.

Subsequently, a process for fresh-water-generating the drinking water s2and the industrial water s3 which are the product waters from thesea-water in the desalination system S, is described.

The sea-water is water-supplied to the UF membrane 3 by the pump p3, andthe particles in the sea-water are removed by permeating the UF membrane3. Thereafter, the UF membrane permeation sea-water s5 b of thesea-water the particles of which have been removed by the UF membrane 3,is water-supplied to the high-pressure RO membrane 4 by the pump p4. Inthe UF membrane permeation sea-water s5 b which has permeated the UFmembrane 3, by permeating the high-pressure RO membrane 4, almost a halfis removed as the sea-water concentrated-water s7 including theimpurities of the salinity, ions or the like, and the remaining half isproduced as the desalinated drinking water s2.

To the contrary, the sea-water concentrated-water s7 of the salinityconcentration of 6 to 8% approximately of approximately ½ in volume ofthe sea-water removed by the high-pressure RO membrane 4 is stirred anddiluted in the stirring-vessel 5 with the sewage waterconcentrated-water s6 (the salinity concentration 0.2% approximately) ofapproximately ½ in volume of the sewage water removed by thelow-pressure RO membrane 2, and the salinity concentration ofapproximately 6 to 8% decreases thereby.

The mixture fluid with decreased the salinity concentrations of thesea-water concentrated-water s7 and the sewage water concentrated-waters6 is water-supplied to the high-pressure RO membrane 6 by the pump p5.

In the mixture fluid of the sewage water concentrated-water s6 and thesea-water concentrated-water s7 from the stirring-vessel 5, bypermeating the high-pressure RO membrane 6, almost a half is removed asthe brine water s9 including the impurities of the salinity, ions or thelike, and the remaining half is produced as the desalinated industrialwater s3.

The desalination system S of the embodiment 1 gives the followingeffects.

1. The sewage water is not mixed in the route for desalinating thesea-water, and the drinking water s2 with a large demand can be producedthereby.2. The sewage water concentrated-water s6 of the brine water removed inthe process of the desalination of the sewage water is added to thesea-water concentrated-water s7 of the brine water removed in theprocess of the desalination of the sea-water, and the industrial waters3 is produced, accordingly, the fresh-water-generation amount of theindustrial water of the entire desalination system S can be increased.

For example, in the desalination system S of the embodiment 1, thesewage water of the amount 2 (volume 2) and the sea-water of the amount2 (volume 2) are supposed to be desalinated.

The industrial water s1 of the amount 1 can be acquired, by permeatingthe low-pressure RO membrane 2, from the sewage water of the amount 2.To the contrary, the drinking water s2 of the amount 1 can be produced,by permeating the high-pressure RO membrane 4, from the sea-water of theamount 2. Furthermore, by stirring the sea-water concentrated-water s7of the amount 1 removed by the high-pressure RO membrane 4 and thesewage water concentrated-water s6 of the amount 1 removed by thelow-pressure RO membrane 2 and permeating the high-pressure RO membrane6, the industrial water s3 of the amount 1 is water-intaken.

As a result, in the desalination system S of the embodiment 1, thedrinking water s2 of the amount 1 and the industrial water s1, s3 of theamount 2 can be acquired, from the sewage water of the amount 2 and thesea-water of the amount 2.

In the case that the sewage water of the amount 2 and the sea-water ofthe amount 2 in the identical condition are desalinated by thedesalination system S100 of the conventional example 1 shown in FIG. 5,it is as following.

As shown in FIG. 5, the sewage water of the amount 2 is desalinated bythe low-pressure RO membrane 102, and the industrial water (the productwater s101) of the amount 1 is produced. Moreover, theconcentrated-water s104 of the sewage water of the amount 1 is added tothe sea-water of the amount 2 in the stirring-vessel 104, therefore, bypermeating the intermediate-pressure RO membrane 105, the sea-water ofthe amount 2 and the industrial water (the product water s102) of theamount 1.5 of ½ of the concentrated-water s104 of the sewage water ofthe amount 1 are produced.

Therefore, in the desalination system S100 of the conventional example1, the product water s101 of the amount 1 and the product water s102 ofthe amount 1.5 are totalized, and the industrial water of the amount 2.5can be acquired.

Accordingly, comparing the desalination system S of the embodiment 1 andthe desalination system S100 of the conventional example 1, thedesalination system S of the embodiment 1 can acquire more drinkingwater of the amount 0.5. Incidentally, in the desalination system S100of FIG. 5, only the industrial water of the amount 2.5 can be acquired,however, the desalination system S of the embodiment 1 has advantages tobe capable of acquiring the drinking water of the amount 1 in additionto the industrial water of the amount 2.

Moreover, in the case to desalinate the sewage water of the amount 2 andthe sea-water of the amount 2 in the identical condition, by thedesalination system S200 shown in FIG. 6 of the conventional example 2,it is as following.

The sewage water of the amount 2 is desalinated by permeating thelow-pressure RO membrane 202 as shown in FIG. 6, and the industrialwater (the product water s201) of the amount 1 can be acquired. To thecontrary, the sea-water of the amount 2 is desalinated by permeating thehigh-pressure RO membrane 205, and the drinking water (the product waters202) of the amount 1 can be acquired.

Therefore, in the case to utilize the sewage water of the amount 2 andthe sea-water of the amount 2, comparing the desalination system S ofthe embodiment 1 and the desalination system S200 of the conventionalexample 2, the desalination system S of the embodiment 1 can acquiremore industrial water of the amount 1.

3. The desalination system S (See FIG. 1) can flexibly correspond to thevariation of the demand of the industrial water, for example, byinterrupting or adjusting the utilization of the sewage waterconcentrated-water s6. Therefore, it is possible to produce theindustrial water, as required, and to correspond to the demand variationof the industrial water.4. In the desalination system S, the sea-water concentrated-water s7 ofthe salinity concentration of 6 to 8% approximately is diluted in thestirring-vessel 5 by the sewage water concentrated-water s6 of thesalinity concentration of 0.2% approximately, accordingly, the salinityconcentration decreases. Therefore, it is possible to utilize thehigh-pressure RO membrane 6 of the same type as the high-pressure ROmembrane 4 in the down-stream side of the sea-water concentrated-waters7.

The higher the salinity concentration is, the higher-pressure ROmembrane is required to be utilized, accordingly, the higher thesalinity concentration is, the higher-pressure power source is required.Therefore, in the case of the sea-water concentrated-water s7 of thesalinity concentration of 6 to 8% approximately, the super-high-pressureRO membrane is required to be utilized, and the power source to outputthe super-high-pressure is required, however, in the desalination systemS of the embodiment 1, the sea-water concentrated-water s7 of thesalinity concentration of 6 to 8% approximately is diluted by the sewagewater concentrated-water s6 of the salinity concentration of 0.2%approximately, therefore, the high-pressure RO membrane can be utilizedand it becomes possible to reduce the power.

5. Furthermore, the high-pressure RO membrane 4, 6 are the same type,therefore, it is easy for the maintenance and the maintainability isfavorable. Accordingly, the advantages for the maintenance management ofthe desalination system S are great.

Embodiment 2

FIG. 2 is a conceptual configuration diagram showing the desalinationsystem of the embodiment 2;

The desalination system 2S of the embodiment 2 has a configuration toomit (without installing) the low-pressure RO membrane 2 of thedesalination system S of the embodiment 1. The other configuration isthe configuration which is similar to the desalination system S of theembodiment 1, therefore, the identical components are shown withidentical references, and the in-depth description is omitted.

In the desalination system 25, the sewage water is water-supplied to theMBR 1 by the pump p1 and permeates the MBR 1, and the activated sludgeflocks, bacteria and the like are removed from the sewage water.Thereafter, the MBR permeable water s22 which has permeated the MBR 1 iswater-supplied to the stirring-vessel 5. In the stirring-vessel 5, theUF membrane 3 is permeated and also the sea-water concentrated-water s7and the MBR permeable water s22 removed by the high-pressure RO membrane4 are stirred and water-supplied to the high-pressure RO membrane 6 bythe pump p5, thereafter.

Here, the sea-water concentrated-water s7 of the salinity concentrationof approximately 6 to 8% is diluted by adding the MBR permeable waters22 of the salinity concentration of approximately 0.1% in thestirring-vessel 5 and the salinity concentration is decreased.

The mixture fluid of the sea-water concentrated-water s7 and the MBRpermeable water s22 is pressurized by the pump p5, and by permeating thehigh-pressure RO membrane 6, a half is removed as the brine water s23including the impurities of the salinity, ions or the like and theremaining half is produced as the desalinated industrial water s21.

In the embodiment 2, the low-pressure RO membrane 2 of the embodiment 1is not installed, therefore, the production and the installation costsof the low-pressure RO membrane 2 are not required, and it is possibleto reduce the cost.

Moreover, the RO membranes (reverse osmosis membranes) are the identicaltype of high-pressure RO membrane 4, 6, therefore, it is easy for themaintenance and the maintainability is further improved. Accordingly,the maintenance manageability becomes more favorable.

Incidentally, the desalination system S of the embodiment 1 gives theaction effects similarly.

<<Variation 1>>

FIG. 3 is a conceptual configuration diagram showing the desalinationsystem of the variation 1.

The desalination system 3S of the variation 1 is made to be aconfiguration to re-utilize the power by providing the energy recoverydevice 34, 36 respectively to the down-stream of the exclusion flow ofthe high-pressure RO membrane 4, 6 of the desalination system S of theembodiment 1.

The other configuration is similar to the configuration of thedesalination system S of the embodiment 1, therefore, the identicalcomponents are shown with identical references, and the in-depthdescription is omitted.

In the desalination system 3S, the sea-water concentrated-water s7removed by the high-pressure RO membrane 4 is pressurized to thehigh-pressure by the pump p4 and has the high pressure energy thereby.

Therefore, in the desalination system 3S, the energy recovery device 34is provided in the flow-channel of the sea-water concentrated-water s7from the high-pressure RO membrane 4.

In the energy recovery device 34, the pressure energy of the sea-waterconcentrated-water s7 removed by the high-pressure RO membrane 4 isrecovered as the rotational energy, then, flows by-passing the pump p4after permeating the UF membrane 3 as the power, and is utilized as thepower to pressure transfer the UF membrane permeation sea-water s31 tothe high-pressure RO membrane 4.

Similarly, because the brine water (the sea-water concentrated-water) s9removed by the high-pressure RO membrane 6 has the high pressure energy,by being pressurized to the high-pressure by the pump p5.

Therefore, in the desalination system 3S, the energy recovery device 36is provided in the flow-channel of the brine water (the sea-waterconcentrated-water) s9 from the high-pressure RO membrane 6.

In the energy recovery device 36, the pressure energy of the brine water(the sea-water concentrated-water) s9 is recovered as the rotationalenergy, then, is given to the stirring-vessel passage water s32 whichflows by-passing the pump p5 after being mixed in the stirring-vessel 5as the power, and is utilized as the power to pressure transfer thestirring-vessel passage water s32 to the high-pressure RO membrane 6.

In the desalination system 3S of the variation 1, the energy recoverydevice 34 is provided in the flow-channel of the down-stream of thesea-water concentrated-water s7 of the high-pressure of the exclusionflow from the high-pressure RO membrane 4 and also the energy recoverydevice 36 is provided in the flow-channel of the down-stream of thebrine water (the sea-water concentrated-water) s9 of the high-pressureof the exclusion flow from the high-pressure RO membrane 6.

The energy recovery device 34, 36 can recover the pressure energy of thesea-water concentrated-water s7 of the high-pressure, the brine water s9respectively as the rotational energy, and can be utilized in the highefficiency condition thereby. Therefore, the reduction of the power(energy) of the desalination system S of the embodiment 1 is possibleand it is possible to achieve the energy conservation.

<<Variation 2>>

FIG. 4 is a conceptual configuration diagram showing the desalinationsystem of the variation 2.

The desalination system 4S of the variation 2 provides the energyrecovery device 44, 46 in the down-stream of the exclusion flow (s41,s42) of the high-pressure RO membrane 4, 6, in the desalination system2S of the embodiment 2, similarly to the variation 1.

The other configuration is similar to the desalination system 2S of theembodiment 2, therefore, the identical components are shown withidentical references, and the in-depth description is omitted.

The desalination system 4S of the variation 2 can recover the pressureenergy of the sea-water concentrated-water s7, the brine water 23 as therotational energy respectively in the energy recovery device 44, 46, andthe pressure transfer power of the UF membrane permeation sea-water s41,the stirring-vessel passage water s42 can be acquired respectively.

In the desalination system 3S of the variation 2, it is possible toreduce the power (energy) of the desalination system 2S of theembodiment 2, and to achieve the energy conservation.

Other Embodiments

Incidentally, in the variation 1, the case to provide both of the energyrecovery device 34, 36 has been exemplified, however, either of theenergy recovery device 34, 36 may be constituted to be provided.Similarly, in the variation 2, the case to provide both of the energyrecovery device 44, 46 has been exemplified, however, either of theenergy recovery device 44, 46 may be constituted to be provided.

Moreover, in the variation 1, the case to utilize the power recovered inthe energy recovery device 34, 36 for the pressure transfer power of theUF membrane permeation sea-water s31, the stirring-vessel passage waters32 respectively has been exemplified, however, it may be utilized forthe other power. Similarly, in the variation 2, the case to utilize thepower recovered in the energy recovery device 44, 46 for the pressuretransfer power of the UF membrane permeation sea-water s41, thestirring-vessel passage water s42 respectively has been exemplified,however, it may be utilized for the power which is different from theexemplified one.

Incidentally, in the aforementioned embodiments and the variations, theMBR has been exemplified as a purification apparatus to remove theactivated sludge from the sewage water and to purify, however, thepurification apparatus which is different from the MBR 1, such as theplain sedimentation method, the sand filtration, the disinfection or thelike, may be applied.

Moreover, the numerical values utilized in the description of theaforementioned embodiments and the variations have shown one example,and these numerical values are not to be limited to.

EXPLANATION OF REFERENCES

-   1 MBR (purification apparatus)-   2 low-pressure RO membrane (first RO membrane)-   3 UF membrane-   4 high-pressure RO membrane (second RO membrane, first RO membrane)-   5 stirring-vessel (stirring apparatus)-   6 high-pressure RO membrane (third RO membrane, second RO membrane)-   34 energy recovery device (first energy recovery device)-   36 energy recovery device (second energy recovery device)-   44 energy recovery device (first energy recovery device)-   46 energy recovery device (second energy recovery device)-   S desalination system (the sea-water desalination system)-   s1, s3 industrial water-   s2 drinking water-   s3 industrial water-   s5 b UF membrane permeation sea-water (treated water)-   s6 sewage water concentrated-water (first concentrated-water)-   s7 sea-water concentrated-water (second concentrated-water, first    concentrated-water)-   s9 brine water (third concentrated-water)-   s21 industrial water-   s22 MBR permeable water (treated water)-   s23 brine water (second concentrated-water)

1. A sea-water desalination method for acquiring industrial water anddrinking water from sea-water and sewage water, removing activatedsludge and purifying by making the sewage water permeate purificationapparatus; producing drinking water by making the sea-water permeate UFmembrane and first RO membrane; and producing industrial water by makingmixture fluid which mixed first concentrated-water removed by the firstRO membrane and the treated water which permeated the purificationapparatus permeate second RO membrane.
 2. A sea-water desalinationmethod according to claim 1, recovering at least either of pressureenergy of the first concentrated-water or pressure energy of secondconcentrated-water removed by the second RO membrane.